CN101929789A - Method for air separation - Google Patents
Method for air separation Download PDFInfo
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- CN101929789A CN101929789A CN2010101708048A CN201010170804A CN101929789A CN 101929789 A CN101929789 A CN 101929789A CN 2010101708048 A CN2010101708048 A CN 2010101708048A CN 201010170804 A CN201010170804 A CN 201010170804A CN 101929789 A CN101929789 A CN 101929789A
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- pressure column
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- lower pressure
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04624—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using integrated mass and heat exchange, so-called non-adiabatic rectification, e.g. dephlegmator, reflux exchanger
- F25J3/0463—Simultaneously between rectifying and stripping sections, i.e. double dephlegmator
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
Abstract
The invention relates to an energy consumption-saving method for air separation; a condensation and evaporation tower is used, and comprises a pressure tower and a lower pressure tower that are arranged in parallel; the pressure tower and the low pressure tower are respectively internally welded with a metal warped piece; the raw material air with absolute pressure 0.30-0.35Mp which is deprivated from moisture and carbon dioxide is pre-cooled to 95-105K; the air enters the pressure tower from the pressure tower raw material air inlet; meanwhile, the valve of the return pipe is switched on to adjust the opening of the valve so that the corresponding gas-liquor separator has a liquid level kept at the set position; when the oxygen-enriched liquid air in the liquid cavity at the bottom of the pressure tower reaches the set height, the liquid air valve is switched on; the oxygen-enriched liquid air at the bottom of the pressure tower is guided out, and is decompressed to 0.13-0.15Mp (absolute pressure); the air enters the low pressure tower through the inlet of the oxygen-enriched liquid air of the low pressure tower; the opening of the liquid air valve enables the oxygen-enriched liquid air in the liquid cavity to be kept at the set position; and oxygen products and nitrogen products are respectively output from the oxygen product outlet and the nitrogen product outlet. The invention is suitable for air separation.
Description
Technical field
The present invention relates to air separating method, particularly adopt the method for condensation-evaporation mode separation of air.
Background technology
Conventional air separating method is with air liquefaction, utilize the difference of component boiling points such as oxygen in the air, nitrogen, argon, separate with the low-temperature fractionating tower oxygen that the air mid-boiling point is higher (normal boiling point 90.17K) nitrogen (normal boiling point 77.35K) lower and argon (normal boiling point 87.219K) etc., obtain the product such as oxygen, nitrogen, argon of required purity with boiling point.
For obtaining the recovery rate of pure oxygen and raising oxygen, generally adopt two stage rectification.Traditional air separation two stage rectification tower is by last, following tower is formed, as shown in Figure 1, a is pressure column (also claiming tower down) among the figure, b is lower pressure column (also deserving to be called tower), s is a condenser/evaporator, its operation principle is: handle raw air premenstruum (premenstrua) of band certain pressure and precooling after bottom the 1 input pressure tower a that enters the mouth, rise along tower internals (column plate or filler), with contact closely along the dirty phegma of tower internals, carry out heat, the matter exchange, make low boiling component (nitrogen) gasification in the liquid phase enter gas phase, and high boiling component (oxygen) condensation in the gas phase enters liquid phase, therefore the continuous enrichment of nitrogen component in the gas uphill process, nitrogen purity has reached requirement (generally more than 99.99%) when arriving cat head, and the middle oxygen content of still liquid (oxygen-enriched liquid air) is not very high (generally containing oxygen 35～40%) at the bottom of the tower.The oxygen-enriched liquid air of pressure column bottom is exported from exporting 9, and secondary rectifying is carried out from the 6 input lower pressure column b that enter the mouth in the decompression back.After the secondary rectifying, lower pressure column top output nitrogen product, lower pressure column bottom its purity of aggregation liquid oxygen has reached requirement (generally more than 99.6%).In the process, the overhead reflux liquid of pressure column and lower pressure column provides by condenser/evaporator s.Condenser/evaporator is arranged between pressure column and the lower pressure column and (is positioned at the lower pressure column place), it has one group of heat exchanger, its effect is that the nitrogen at pressure column top is drawn and is condensed into liquid nitrogen from exporting 2, this liquid nitrogen is from exporting 7 outputs, wherein a part participates in rectifying from the 8 input pressure tops of tower that enter the mouth as the pressure column phegma, and another part decompression back participates in secondary rectifying from the 5 input lower pressure column tops that enter the mouth as the lower pressure column phegma.The nitrogen condensation is an exothermic process, and the heat of release makes the liquid oxygen gasification of lower pressure column bottom, and from exporting 3 outputs, another part participates in rectifying as the rising steam of lower pressure column bottom to a gained oxygen part as oxygen product.Because the boiling point of nitrogen is lower than the boiling point of oxygen under uniform pressure, so if the operating pressure of pressure column and lower pressure column is identical, then heat can't be passed to the oxygen side of high temperature from the nitrogen side of low temperature, realize the nitrogen condensation of above-mentioned pressure column top, lower pressure column bottom oxygen evaporating course, must improve the nitrogen lateral pressure, the nitrogen boiling point is improved and the realization condensation, and will keep certain heat transfer temperature difference.If lower pressure column bottom liquid oxygen evaporation average operating pressure is 0.136Mpa (absolute pressure), mean temperature difference is 0.8K, then require the condensing pressure of pressure column top nitrogen to remain on more than the 0.5Mpa (absolute pressure), consider the resistance of air treatment facility in early stage and pipeline, the pressure at expulsion of final raw air machine will reach 0.53Mpa (absolute pressure) at least, and this is the most dominant energy consumption of this air-separating plant.So the air-separating plant energy consumption of traditional upper and lower tower structure is bigger.
Summary of the invention
The present invention will solve prior art and adopt the big problem of cryogenic rectification method separation of air energy consumption, the method of a kind of air separation of the present invention is provided for this reason, pressure column and lower pressure column that this method adopts closing arranged side by side to be provided with, can utilize between two tower media heat to transmit naturally and optimize distillation process, reach the effect that cuts down the consumption of energy.
For addressing the above problem, its special character of the technical solution used in the present invention is to adopt the condensation evaporation tower to make air separation, and described condensation evaporation tower is made up of pressure column and lower pressure column that closing arranged side by side is provided with, respectively is welded together with metal fin in pressure column and the lower pressure column;
The phegma outlet is established in the sealing of pressure column end face, pressure column, and this phegma outlet is connected with gas-liquid separator through pipeline section, and pressure column is established the raw air import in the bottom, and pressure column is established the oxygen-enriched liquid air reservoir compartment in the bottom;
Lower pressure column bottom lock, lower pressure column are established phegma import and expanded air import, and the oxygen-enriched liquid air import is established at the lower pressure column middle part, and the oxygen product outlet is established in the lower pressure column bottom, and the nitrogen products export is established at the lower pressure column top;
Pressure column bottom reservoir compartment leads to through the oxygen-enriched liquid air import of pipeline section and lower pressure column, the liquid phase outlet of described gas-liquid separator is led to through the described phegma import of return duct and lower pressure column, described return duct is provided with valve, and the gaseous phase outlet and the pressure column of gas-liquid separator lead to;
The lower pressure column oxygen-enriched liquid air import connecting leg Duan Shangshe of institute liquid air valve;
The step of described air separation is:
---with absolute pressure is that the raw air that removes moisture and carbon dioxide of 0.30～0.35Mpa is chilled to 95～105K in advance, from pressure column raw air import input pressure tower, meanwhile, open valve set on the described return duct, regulate the aperture of this valve, make liquid level maintenance desired location in the corresponding described gas-liquid separator;
---when oxygen-enriched liquid air reaches setting height in the oxygen-enriched liquid air reservoir compartment of pressure column bottom, open the liquid air valve, 0.13～0.15Mpa (absolute pressure) is drawn and be decompressed to the oxygen-enriched liquid air of pressure column bottom, by the oxygen-enriched liquid air import input lower pressure column of lower pressure column, the aperture of liquid air valve is to make the interior oxygen-enriched liquid air of pressure column oxygen-enriched liquid air reservoir compartment keep described desired location;
---expanded air is from expanded air import input lower pressure column;
---oxygen product, nitrogen product are respectively from oxygen product outlet, the output of nitrogen products export.
Pressure column of the present invention is established phegma outlet and is meant that pressure column establishes No. zero outlet from top to bottom in nearly top, in rectifying section establish an outlet, export for No. two ... with N number outlet; Described lower pressure column establish the phegma import be meant the lower pressure column top establish No. zero import and establish from top to bottom an import, No. two imports ... with the N import; The outlet of the liquid phase of described gas-liquid separator is led to through the phegma import of return duct and lower pressure column, be meant pressure column No. zero outlet, an outlet, export for No. two ... the liquid phase that connects gas-liquid separator with N number outlet institute export through return duct correspondingly with the zero number import of lower pressure column, an import, No. two imports ... import is led to N; Described return duct is provided with valve, be meant respectively with No. zero import, an import, No. two imports ... with No. zero valve set on the N import institute connecting leg section, valve, No. two valves ... with the N valve.
Described No. zero outlet, an outlet, No. two outlets ... with N number outlet, and described No. zero import, an import, No. two imports ... with the N import, in " ... and N " being meant the set of number of arranging by natural ordinal number, it depends on the theoretical cam curve of pressure column and lower pressure column.The position of these outlets, import, corresponding with the height equivalent to a theoretical stage (plate) of pressure column, lower pressure column.Theoretical tray is computable in the design, so the position of described " ... and N " and " outlet ", " import " is to determine.The position of lower pressure column phegma import is arranged at the concentration corresponding position with the outlet of pressure column phegma, in other words, the material component concentration of lower pressure column phegma import corresponding position, the material component concentration of corresponding pressure column phegma outlet corresponding position of leading to this import is suitable.
The metal fin that weldering is established in described pressure column, the lower pressure column has upper and lower passage and has big specific area, and its effect one is as fractional distillation filling-material, caloic exchange between gas, liquid in the accelerated tower, and the 2nd, transmit media as heat between pressure column, lower pressure column.
The invention will be further described below in conjunction with accompanying drawing.
Description of drawings
Fig. 1 is prior art air separation rectifying column structure and schematic flow sheet;
Fig. 2 is air separation of the present invention condensation evaporation column structure and a schematic flow sheet.
Be labeled as among the figure: 1 inlet, 2 outlets, 3 outlets, 4 expanded airs inlet, 5 inlets, 6 inlets, 7 outlets, 8 inlets, 9 outlets, a pressure column, b lower pressure column, s condenser/evaporator; The P pressure column, L lower pressure column, the import of A raw air, B reservoir compartment, the outlet of C oxygen product, the import of D oxygen-enriched liquid air, E nitrogen products export, the F gas-liquid separator, the import of K expanded air, No. zero outlet of C0, an outlet of C1, Cn N number outlet, R0 No. zero import, an import of R1, Rn N import, V0 No. zero valve, valve of V1, Vn N valve, Vd liquid air valve.
In the work, after raw air enters pressure column P, as the rising steam along conducting heat to lower pressure column L by tower internals in tower internals (metal fin) uphill process, the uprising gas partial condensation becomes the phegma of pressure column, and the phegma of lower pressure column partly evaporates and becomes its rising steam, and the distillation process of pressure column and lower pressure column just can continue to carry out like this. In gas-liquid two-phase close contact process, lower boiling nitrogen component is constantly evaporated and is entered gas phase in the liquid phase, and the simultaneously higher continuous condensation of oxygen component of gas phase mid-boiling point enters liquid phase. The top of pressure column obtains the purity nitrogen of purity more than 99.99%, and the bottom obtains oxygen content and is about 35% oxygen-enriched liquid air. This oxygen-enriched liquid air carries out secondary rectifying by the rear input of liquid air valve Vd decompression lower pressure column middle part as raw material. Pressure column is sent into input lower pressure column top after separating the liquid nitrogen decompression of obtaining except the top condensation and through gas-liquid separator F, participate in outside the secondary rectifying as the lower pressure column phegma, pressure column also causes lower pressure column as the lower pressure column phegma in rectifying section after a height equivalent to a theoretical stage (plate) is with the decompression of partial reflux liquid.
The closing setting arranged side by side and mutual of pressure column of the present invention and lower pressure column, lower pressure column bottom liquid oxygen can utilize the heat of pressure column bottom oxygen-enriched air condensation release and evaporate, divide rectifying column to compare with the sky of the upper and lower tower structure of tradition, the concentration difference of condensation evaporation tower media of both sides of the present invention reduces, become oxygen enrichment (gas) condensation and pure oxygen (liquid oxygen) evaporation by purity nitrogen (nitrogen) condensation and pure oxygen (liquid oxygen) evaporation, the operating pressure of condensation side (being pressure column) is descended, reach energy-conservation purpose. If lower pressure column bottom liquid oxygen evaporating pressure is that 0.136Mpa (absolute pressure) and both sides (pressure column-lower pressure column) heat transfer temperature difference are 0.8K, pressure column bottom operating pressure is reduced to about 0.32Mpa (absolute pressure), when determining the raw air pressure at expulsion because counting the resistance of pressure column, so finally the pressure at expulsion of raw air can be dropped to about 0.35Mpa (absolute pressure), reach the purpose that cuts down the consumption of energy.
The operating temperature of pressure column and lower pressure column depends on the boiling point of its medium, and the boiling point of medium is relevant with operating pressure and concentration of component, so as long as the just operation of energy control tower of the operating pressure of two towers of control. The operating pressure of lower pressure column depends on the flow resistance of the gas discharge process such as oxygen, nitrogen, this resistance is substantially definite when design, change little in the operation, the average operating pressure of general lower pressure column is about 0.14Mpa (absolute pressure), so the temperature of each height section of lower pressure column changes with component, is the boiling point of oxygen under this operating pressure at the bottom of the tower, cat head is the boiling point of nitrogen, the centre is the boiling point of each section component, and relatively stable needn't deliberately controlling. And the operating temperature of pressure column has determined the heat transfer temperature difference to lower pressure column, this heat transfer temperature difference determines the size of condensation number and evaporation capacity, namely determine the quality of condensation evaporation tower operation, so the operating pressure of pressure column is most important operating parameter, the raw air absolute pressure of input pressure tower of the present invention is 0.30～0.35Mpa.
The present invention has not only reduced the operating pressure of the operating pressure while energy automatic pressure regulation tower of pressure column, its regulation mechanism is as follows: take when the operating pressure of pressure column is higher than institute, the corresponding raising of the boiling point of medium meeting in the pressure column, the temperature of the each point of lower pressure column is metastable as mentioned above, like this, because improving, the temperature of pressure column will make the heat transfer temperature difference of two towers big, the condensation number of medium in the pressure column is increased, but the discharge capacity of raw material air compressor machine is fixed, just make the pressure drop of pressure column, on the contrary, such as the hypotony of pressure column, then the temperature difference reduces to make the medium condensation number to reduce, and the operating pressure of pressure column gos up, finally can autobalance arrive required operating pressure, keep the minimum heat transfer temperature difference between two towers.
The present invention is owing to the tower internals (metal fin) as heat transfer element has big specific area and all can arrange this tower internals on whole height of tower, so the heat transfer area between two towers is very big, make the minimum temperature difference between two towers can maintain quite little level, even can be less than 0.3K, the operating pressure of pressure column can further reduce like this.
The a little higher than lower pressure column of the temperature of pressure column forms heat transfer temperature difference. Medium in the pressure column by tower internals constantly to the medium transferring heat of lower pressure column side, because the medium in two towers all is in saturation state, so condensation constantly takes place in the medium in the pressure column, build-up of pressure reflux in tower liquid surplus, on the contrary, medium in the lower pressure column is heated and constantly evaporates, cause the phegma deficiency, for solving this contradiction, extraction force tower variable concentrations of the present invention position (described No. one the outlet, No. two the outlet ... with N number outlet corresponding position) unnecessary liquid, input lower pressure column corresponding concentration position replenishes the lower pressure column phegma after the decompression.
The part that expanded air of the present invention input lower pressure column, this expanded air can be used as raw air enters lower pressure column and participates in rectifying, also can form one independently kind of refrigeration cycle only do not participate in rectifying for device provides the cold of cryogenic conditions.
The specific embodiment
Embodiment one
Condensation evaporation tower shown in the employing figure two is made air separation, and this condensation evaporation tower is made up of pressure column 1 and lower pressure column 2 that closing arranged side by side is provided with, respectively is welded together with metal fin in pressure column and the lower pressure column;
The lower pressure column bottom lock, lower pressure column is established the phegma import, be the lower pressure column top establish No. zero import R0 and establish from top to bottom an import R1, No. two imports ... with N import Rn, lower pressure column is also established expanded air import K, oxygen-enriched liquid air import D is established at the lower pressure column middle part, oxygen product outlet C is established in the lower pressure column bottom, and nitrogen products export E is established at the lower pressure column top;
Pressure column bottom reservoir compartment B leads to through the oxygen-enriched liquid air import D of pipeline section and lower pressure column, the outlet of the liquid phase of described gas-liquid separator F is led to through the described phegma import of return duct and lower pressure column, i.e. pressure column No. zero outlet, an outlet, export for No. two ... the liquid phase that connects gas-liquid separator with N number outlet institute export through return duct correspondingly with the zero number import of lower pressure column, an import, No. two imports ... import is led to N; Described return duct is provided with valve, promptly respectively with No. zero import, an import, No. two imports ... with N import connect set No. zero valve V0 on the return duct, valve V1, No. two valves ... with N valve Vn; The gaseous phase outlet and the pressure column of gas-liquid separator lead to;
The lower pressure column oxygen-enriched liquid air import connecting leg Duan Shangshe of institute liquid air valve Vd;
The step of described air separation is:
---with absolute pressure is that the raw air that removes impurity such as moisture, carbon dioxide of 0.30Mpa is chilled to 95K in advance, from pressure column raw air import A input pressure tower 1, meanwhile, open valve set on the described return duct, regulate the aperture of this valve, make liquid level maintenance desired location in the corresponding described gas-liquid separator F;
---when oxygen-enriched liquid air reaches setting height in the oxygen-enriched liquid air reservoir compartment B of pressure column bottom, open liquid air valve Vd, 0.13Mpa (absolute pressure) is drawn and be decompressed to the oxygen-enriched liquid air of pressure column bottom, by the oxygen-enriched liquid air import D input lower pressure column of lower pressure column, the aperture of liquid air valve Vd is to make the interior oxygen-enriched liquid air of pressure column oxygen-enriched liquid air reservoir compartment keep described desired location;
---expanded air is from expanded air import K input lower pressure column;
---oxygen product, nitrogen product are respectively from oxygen product outlet C, nitrogen products export E output.
Embodiment two
This example is to be that the raw air that removes impurity such as moisture, carbon dioxide of 0.32Mpa is chilled to 100K in advance with absolute pressure, from pressure column raw air import A input pressure tower 1, meanwhile, open valve set on the described return duct, regulate the aperture of this valve, make liquid level maintenance desired location in the corresponding described gas-liquid separator F; When oxygen-enriched liquid air reaches setting height in the oxygen-enriched liquid air reservoir compartment B of pressure column bottom, open liquid air valve Vd, 0.14Mpa (absolute pressure) is drawn and be decompressed to the oxygen-enriched liquid air of pressure column bottom, by the oxygen-enriched liquid air import D input lower pressure column of lower pressure column, the aperture of liquid air valve Vd is to make the interior oxygen-enriched liquid air of pressure column oxygen-enriched liquid air reservoir compartment keep described desired location.Other are identical with last example.
Embodiment three
This example is to be that the raw air that removes impurity such as moisture, carbon dioxide of 0.35Mpa is chilled to 105K in advance with absolute pressure, from pressure column raw air import A input pressure tower 1, meanwhile, open valve set on the described return duct, regulate the aperture of this valve, make liquid level maintenance desired location in the corresponding described gas-liquid separator F; When oxygen-enriched liquid air reaches setting height in the oxygen-enriched liquid air reservoir compartment B of pressure column bottom, open liquid air valve Vd, 0.15Mpa (absolute pressure) is drawn and be decompressed to the oxygen-enriched liquid air of pressure column bottom, by the oxygen-enriched liquid air import D input lower pressure column of lower pressure column, the aperture of liquid air valve Vd is to make the interior oxygen-enriched liquid air of pressure column oxygen-enriched liquid air reservoir compartment keep described desired location.Other are identical with example one.
Claims (2)
1. the method for an air separation is characterized in that adopting the condensation evaporation tower to make air separation, and described condensation evaporation tower is made up of pressure column (1) and lower pressure column (2) that closing arranged side by side is provided with, respectively is welded together with metal fin in pressure column and the lower pressure column;
The phegma outlet is established in the sealing of pressure column (1) end face, pressure column, and this phegma outlet is connected with gas-liquid separator (F) through pipeline section, and pressure column is established raw air import (A) in the bottom, and pressure column is established oxygen-enriched liquid air reservoir compartment (B) in the bottom;
Lower pressure column bottom lock, lower pressure column are established phegma import and expanded air import (K), and oxygen-enriched liquid air import (D) is established at the lower pressure column middle part, and oxygen product outlet (C) is established in the lower pressure column bottom, and nitrogen products export (E) is established at the lower pressure column top;
Pressure column bottom reservoir compartment (B) leads to through the oxygen-enriched liquid air import (D) of pipeline section and lower pressure column, the liquid phase outlet of described gas-liquid separator (F) is led to through the described phegma import of return duct and lower pressure column, described return duct is provided with valve, and the gaseous phase outlet and the pressure column of gas-liquid separator lead to;
The lower pressure column oxygen-enriched liquid air import connecting leg Duan Shangshe of institute liquid air valve (Vd);
The step of described air separation is:
---with absolute pressure is that the raw air that removes moisture and carbon dioxide of 0.30～0.35Mpa is chilled to 95～105K in advance, from pressure column raw air import (A) input pressure tower (1), meanwhile, open valve set on the described return duct, regulate the aperture of this valve, make the interior liquid level of corresponding described gas-liquid separator (F) keep desired location;
---when oxygen-enriched liquid air reaches setting height in the pressure column bottom oxygen-enriched liquid air reservoir compartment (B), open liquid air valve (Vd), 0.13～0.15Mpa (absolute pressure) is drawn and be decompressed to the oxygen-enriched liquid air of pressure column bottom, by oxygen-enriched liquid air import (D) the input lower pressure column of lower pressure column, the aperture of liquid air valve (Vd) is to make the interior oxygen-enriched liquid air of pressure column oxygen-enriched liquid air reservoir compartment keep described desired location;
---expanded air is from expanded air import (K) input lower pressure column;
---oxygen product, nitrogen product are respectively from oxygen product outlet (C), nitrogen products export (E) output.
2. the method for a kind of air separation as claimed in claim 1, it is characterized in that described pressure column establishes phegma outlet and be meant that pressure column establishes No. zero outlet (C0) from top to bottom in nearly top, in rectifying section establish an outlet (C1), export for No. two ... with N number outlet (Cn); Described lower pressure column establish the phegma import be meant the lower pressure column top establish No. zero import (R0) and establish from top to bottom an import (R1), No. two imports ... with N import (Rn); The outlet of the liquid phase of described gas-liquid separator (F) is led to through the phegma import of return duct and lower pressure column, be meant pressure column No. zero outlet, an outlet, export for No. two ... the liquid phase that connects gas-liquid separator with N number outlet institute export through return duct correspondingly with the zero number import of lower pressure column, an import, No. two imports ... import is led to N; Described return duct is provided with valve, be meant respectively with No. zero import, an import, No. two imports ... with N import connect set No. zero valve (V0) on the return duct, a valve (V1), No. two valves ... with N valve (Vn).
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| CN2010101708048A CN101929789B (en) | 2010-05-12 | 2010-05-12 | Method for air separation |
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| CN200955890Y (en) * | 2006-09-08 | 2007-10-03 | 浙江大学 | Internal thermal coupled air separation plant |
| JP2009014311A (en) * | 2007-07-09 | 2009-01-22 | Taiyo Nippon Sanso Corp | Air separation method and device |
| CN201413000Y (en) * | 2009-06-02 | 2010-02-24 | 武汉钢铁(集团)公司 | Novel air separation device |
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2010
- 2010-05-12 CN CN2010101708048A patent/CN101929789B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| EP1230522A1 (en) * | 1999-08-24 | 2002-08-14 | L'air Liquide, S.A. à Directoire et Conseil de Surveillance pour l'Etude et l'Exploitation des Procédés Georges Claude | Evaporator-condenser and corresponding air distillation installation |
| CN1878998A (en) * | 2003-11-10 | 2006-12-13 | 液体空气乔治洛德方法利用和研究的具有监督和管理委员会的有限公司 | Method and installation for supplying highly pure oxygen by cryogenic distillation of air |
| US20050274142A1 (en) * | 2004-06-14 | 2005-12-15 | Corey John A | Cryogenically producing oxygen-enriched liquid and/or gaseous oxygen from atmospheric air |
| CN200955890Y (en) * | 2006-09-08 | 2007-10-03 | 浙江大学 | Internal thermal coupled air separation plant |
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| Publication number | Publication date |
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| CN101929789B (en) | 2012-07-18 |
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